Apparatus and method for handling of liquefied normally gaseous materials



Sept. 2, 1 J. s. HAUG ETAL APPARATUS AND METHOD FOR HANDLING OFLIQUEFIED NORMALLY GASEOUS MATERIALS 2 SHEETS--SHEE'I 1 Filed Dec. 51,1946 R O T NG m WH S N H O v PRICE WJANEMWJR BY THEIR ATTORNEYS W6-Sept. 2, 1952 -J. s. HAUG ET AL 2,609,282

APPARATUS AND METHOD FOR HANDLING OF LIQUEFIED NORMALLY GASEOUSMATERIALS Filed Dec. 31, 1946 2 SHEETSSHEE'I 2 Ill TTT w 75 M72, 40:521.INVENTOR 0 /07 JOHN S,HAUG

PRICE WJANEWAYJR.

BY THEIR ATTORNEYS /5@ZOW7V&

l ate'n ted Sept. 2

OF LIQUEFIED NORMALLY GAS-EOUS MA- TERIALS John S. Haug, Philadelphia,and Price W. J aneway, Jr., Media, Pa., assignors to United Engineers &Constructors Inc., Philadelphia, Pa., a corporation of DelawareApplication December 31, 1946, Serial No. 719,348

4 Claims. IV The present invention relates to the handling of liquidshaving a relatively high vapor pressure under the conditions obtaining.

An example of such handling is the'transportation through pipes exposedto atmospheric 5 pane vapor, small dififerences in percentage ofconditions of liquid phase material normally evaporation by weightresulting in great difier'f gaseous under such conditions. ences in theproportion of vapor present by vol- For purposes of illustration, theinvention will ume. Such a mixture cannot be accurately" be particularlydescribed in connection with its metered by presently available liquidor vapor application to the piping and utilization of liquemeters, withthe result that the rate of utilizafied normally gaseous hydrocarbonssuch as protion of the material may not be accurately known pane andbutane, which are frequently employed or ascertained. as raw materialsin the manufacture of com- One of the objects of the present inventionis bustible gas. to provide a method of and apparatus for the One of theuses of such liquefied normally delivery through pipes of liquidmaterial of relgaseous hydrocarbon material in the manufacatively highvolatility under the ambient conture of combustible gas, is in thesupplementing, ditions, in the use of which the liquid material 1 duringperiods of peak loads, of the carburetted delivered to a zone ofutilization, treatment, or water gas normally produced in carburettedother disposal may be accurately metered in spite water gas sets fromsolid fuel and heavier hyof the formation of vapor phase occurring as adrocarbon oils. necessary incident to a drop in pressure in the Suchutilization of liquefied normally gaseous transportation system. Otherobjects of the inhydrocarbons frequently includes the cracking ofvention will appear as the specification proceeds. these materials bypassage through the fuel bed For co e c e i v ntion Will be more. of thewater gas generator in a step commonly particularly described inconnection with the termed reforming, and may also include a step p p 0fliquefied P p rom Storage under of utilizing these materials forenrichment withpressure to utilization in the manufacture of car-' outmaterial cracking. buretted water gas, and in connection with the It iseconomical from the standpoint of the description of the figures, whichform a part of investment costs to store hydrocarbon materials thisspecifi and in which such as propane .and butane as liquids under Figure1 WS. Somewhat at c l y. relatively elevated pressure because of thegreatp y in elevation and p y in Vertical Seetion,v 1y reduced size ofthe storage equipment rea carburetted water gas set suppliedwith andquird to store these materials in gaseous form. utilizing liquefiedpropane in accordance with a.- It is also economical from the standpointOf 111- form of the present invention chosen for illusvestment totransport these materials in liquid t t form, from storage to a pointadjacent the g Figure 2 shows, somewhat diagrammatically, ggggg g ilgfi? gifii gg gg g p gg fgg fig partly in elevation and partly invertical section, as compared with that required to transport 40 gfig iof the apparatus of the mventmn'. them as gases. r 3 h h Such liquidstorage is customarily exposed to lgur'e T 0W5 aflpor {on of t eapparatus I existing atmospheric temperature conditions and Flgure WlthP F QS' therefore the storage of the liquid usually oc- Referrmg Ftlgure1: curs under a very considerable pressure due to generally mdlca'testhe generator 2 the car? 7 this temperature. For example, in the case ofbummer 3 the Superheater a 4 the Wash commercial liquid propane, at say30 F. the 0f ealburetted Water gas Setvapor pressure will be of theorder of 100 pounds The generator is pr vid d wit an i nited fuel persquare inch absolute, while at 72 F. the bed 5, ofsolid fuel,-such ascoke, resting on a; vapor pressure will be of the order of 160 pounds grt (not O D- The ator is furt er I per square inch absolute. Since theliquid in provided with air supply means and steamsup l storage is inequilibrium under the existing storply means 6 and 1 respectively, forupwardly air" age pressure and the existing atmospheric temblasting Steag the fuel bed. The gen perature, any pressure difierential causing afiow erator is also illustrated as provided with sec.- of the liquidfrom storage will cause the evapo- 2 r ration of a portion thereof. As aresult, the material passing through the pipe leading from the storagevessel toward the point of utilization is a varying mixture of liquefiedpropane and proondary air supply means 8 and oil supply means 3 9arranged to spray oil onto the top of the fuel bed.

The generator is further illustrated as provided with a gas take-offconnection 10, leading from its upper portiorrto the upper portion ofthe carburetterZ, and with the gas take-off H, provided with valve Ila,and leading from its lower portion below the grate to the wash box 4.

The carburetter is illustrated as devoid of checker-brick, but providedwith the refractory lining l2. [3 indicates an oil supply means arrangedto spray oil into the carburetter. The base of the carguretter isillustrated as connected with the base of the superheater by theconnection The superheater is illustrated as provided with refractorychecker-brick l5, stack valve l6, and gas take-01f IT, provided withvalve Ila, and leading from the upper portion of the superheater to thewash box 4. The superheater is further illustrated as provided withsteam supply It; fer back-running.

.In Fig. 1, the operating connection indicated between valves I la andma is intended to be diagrammatic, the connection being such that theopening or closing respectively of one valve by the hydraulic cylinderl'lb is accompanied by the clesing or opening respectively of the other.

Thewash box 4 is illustrated as provided with thesealing liquid supplyl9 and the liquid overflow 20, which are adapted to provide a liquidseal for dippipe 21, which is connected with the pipes H and I1 leadingfrom the generator base and superheater top respectively. The valvedgastake-off 22, provided with valve 22a, leads from the wash box to thegas take-off main 23, which leads to storage, condensing andpurification apparatus (not shown).

25' generally indicates a pressure storage tank for, liquefied propane,which is to be supplied in metered quantities to the carburetted watergas set as desired.

@Inaccordance with the form of the invention chosen 'for illustration,liquefied propane is caused to flow from the storage tank 25, throughpipe'2B to a phase separating vessel 21 in response'to' a pressuredifferential therebetween. If desire'jd, pipe'26 may be provided witheither the hand operated throttling valve 28, or the automaticallyoperated reducing valve 29, or

both.

The function of the phase separating chamber 21 is'to cause theseparation from each other of liquefied propane passed from storagethrough pipe'2B and propane vapor produced in transit by evaporationincidental to the drop in pressurethrough pipe 26 including valves 28and 29, if provided. The material flows into chamber 21 in a chilledcondition due to this evaporation. Propane vapor separated in chamber 27passes byway of pipe 30, provided with valve 3|, to the gas take-01fmain 23, and is illustrated as metered en route by the vapor meter32.

Liquid propane separated in chamber 27 is delivered by pump 33 ,by wayof pipes 34 and 35 to the water gas set, passing through the liquid,

header 36, whichmay supply'a plurality of gas sets, and through pipe 37to the particular water set shown, entering the top of the superheater'3, with the back-run steam, supplied through [8.

Pipe 31 may be provided with the regulating valve 38,for regulating theflow of liquid propane tothe set and with the hydraulic operating valve39*forcontrolling the admission of liquid propane '4 thereto during thedesired periods of a cycle, for example, as controlled by the usualautomatic controlled machine.

Liquid meter 40 is arranged in pipe ,31 for metering the liquid propane:flowing therethrough to the gas set. 4| is a shut-off valve, the closingof which disconnects pipe 31 from the liquid header 36.

.The phase separating vessel 21 is illustrated as provided withthe floatchamber 42 and with the float 43, which is operably connected with thevalve 3! in the vapor line from the phase separating vessel in suchmanner that should the float 43 sink, due to a lowering of the level ofthe liquid propane in chamber 21, the valve 3| will be moved toward thewide-open position, thereby increasing the flow of vapor from chamber21, through pipe 30, to the gas take-01f main 23. Vice versa, shouldfloat 43 rise because of the rising of the level of the liquid propane.in chamber 21, valve 3| will be moved toward the closed'position,thereby reducing the flow of Va; por through pipe 30.

The automatic reducing valve 29, which may or may not be provided asdesired, isilIuStrated as 'operably connected, asby pipe 44, withchamber 27, in such manner as to be responsive to changes of pressurewithin the chamb er,'increas-. ing pressure in chamber'Z'l tendingtomove valve 29 toward the closed position and decreasing pressure inchamber 21 tending .to move valve 29 toward the wide-openposition.

The following is given as an illustrative ex: ample of the operation .ofthe form of the apparatus of the invention chosen for illustration inFigure '1, bearing in mind that'its usein con-i nection with thehandling.of propane specifically and its use in connection with the specificuti-. lization of the conveyed liquidin a carburetted water gas set arepurely for purposes of illus-r. tration. The invention,,in its broaderaspects,.is not limited to the conveying of any particular liquid of thegeneral character described nor to any particular utilization,treatmentor other dis-. posal of the liquid delivered.

The ignitedfuel bed 5 in generator .I alter-. nately blasted with airand steam in a cyclic operation.

During the air blasting step of thecycle, termed the blow, with valve Haclosed and the stack valve it open, air blast admitted through airsupplyimeans 6 raises the fuel bed to ahigh temperature and stores heattherein. The resulting producer gas issuing from the top of .the fuelbed is burned with secondary air admitted throughair supply 8.The'burning producer gas and the resultingproducts of combustiontraverse the carburetter and superheater, storing heatin the refractoryliningsand checker-brick thereof and issue to the atmosphere throughthestack" valve 16.

After the .fuel bed and the. carburetterand; superheater have been.raisedto the desired .tem peratures, the blow is terminated, the

water gas generating period termed the run? is,

begun. With valve 1 i remainingmlosfid; steam, is admitted-to the baseor thegeneratqr through steam supply I, for reactionwith the,ignitediuel: bed to produce water gas. The resulting up-. run water gaspasses from the top of the-fuel bed through connection Ill to thecarburetter, thence through connection (4 tothe superheater,

The stack valve I6 is closed shortly after the.

beginning of the steaming operation, that israfterthe up-run water gashas purged'through the' 5. stack, the combustion products of the airblast remaining in the set at the end of the air blasting operation.After this purge with valve 11a in pipe I! open, the up-run gas passesthrough pipes l1 and 2| to wash box 4 and thence through take-ofi 22 andvalve 22a to take-off main23.

During the up-run, the blue water gas pass-- ing through the carburetterand superheater is carburetted with oil gas produced by-spraying.

oil into the top of the generator through oil supply 9 and/or into thetop of the carburetter through oil supply 13, the heat stored during the"blow serving to vaporize the oil and to crack theresulting oil vaporsin the presence of the blue water gas and excess steam from thegenerator.

After the up-run, the admission of steam through supply I is ceased andthe valves Ila and Ila are reversed. Steam is admitted through steamsupply l8 and passed reversely through the superheater, carburetter andgenerator, and the resulting back-run" water gas passed to the wash boxby way of pipe II from the base of the generator and thence by way ofconnection 22 to the gas take-01f main 23.

After the termination of the back-run, the valves Ila and Ila are againreversed, and a short up-run is made with steam supplied to the base ofthe generator through steam supply 1.

Following this up-run, the cycle is repeated,

by the initiation of another air blasting operation,

the stack valve It not being opened until the products of combustionhave pushed the carburetted water gas, remaining in the set at the endof the run, out of the set through connection IT.

The foregoing description of the operation of a carburetted water gasset was chosen purely for illustration and may be widely varied.

For the purpose of conveniently increasing the output of a carburettedwater gas set during periods of peak loads, it has been proposed tosupplement the gas production, from solid fuel and from the conventionalenriching oils, with gas produced by the vaporization and/or thevaporization and pyrolysis of liquefied normally gaseous hydrocarbonssuch as propane and butane.

In the embodiment of the present invention illustrated in Figure 1,during the back-run, liquid propane is pumped from the phase separatingchamber 2'! by pump 33 through pipe 35, liquid header 36, liquid meterWand pipe 3'1 into connection I! in the proximity of the superheatertop, to which the steam is simultaneously admitted through steam supply'23. The result;

steam and gas resulting from the pyrolysis of the propane vapor, passthrough the back-run pipe I] to the wash box 4 and thence to the gastakeofi main 23. V

Simultaneously the vapor phase propane separated in the phase separatingchamber 2! may be passed by way of pipe 39, valve 3|, and the'vapormeter 32 into the gas take-off main 23, serving as cold enrichment ofthe gas produced in the set.

At the end of the back-run, the carburetter and superheater are full ofpropane vapor resulting from the evaporation of .theliquidpropane f.

cracked by passage through the fuel bed. zi Ihis .1 vapor'phase propaneis pushed through. the wash box into the gas take-off main by thesucceeding up-run gas, and also serves as enrichment.

According to the embodiment of the invention illustrated in Figure 1,the mixture of liquid and vapor. phase propane, produced by theevaporation due to drop in pressure as the liquid propane flows fromstorage tank 25,-isseparated into the respective liquid and vapor phasesin chamber 21. The separated liquid phase ispumped by pump 33 throughthe liquid meter 40 under a sufhciently elevated pressure .sothat'whenthe liquid propane passes through the liquid meter the. temperature ofthe propane is below its boiling point under said elevated pressure.

In case the liquid phase material is a mixture,

the. pressure at the liquid meter is preferablysuch that the temperatureobtaining is below the boiling point ofathe lowest boiling constituentthereof. v

The pressure is preferably such as to preclude the presence of anysubstantial proportion, by-volume, of vapor phase with'the separatedliquid material as it passes through said-liquid meter, in spite of anypressure drop or rise of temperature which may occur between thezpumpand the liquid meter. I

Since the evaporation of a portion of the liquid propane. due topressure drop in the passage from the storage tank to the phaseseparating chamber abstracts heat from the remaining liquid phasematerial. reducing its temperature, the pressure developed by pump 33,therefore,

need only be sufilcient to maintain the chilled liquid in the liquidphase up to and through the liquid meter as described.

In the apparatus illustrated in Figure 1, connection 28 leading from thestorage tank to the phase separator is shown provided with a handoperated throttling valve and with an automati-- cally operated reducingvalve. Either or both to produce a selected pressure drop in line 26,-and the automatically operated reducing valve may be desired to maintaina constant pressure drop therein.

As stated, however, either or both of these valves may be omitted. Inthe absence of reducing valve 29 and its operating connection 44, anyloweringof the level of the liquid in chamber 21 moves valve 3| towardthe wide-open position, and by bleeding vapor from chamber 21 reducesthe pressure therein, which in turn increases the difierential pressurebetween the storage tank and the chamber 21, thereby increasing the flowof material through line 26 to restore the liquid level in chamber 21.Any increase in the height of the liquid'level in chamber 2! isaccompanied by the reverse operation of the float 43 and valve 3!, whichincreases the pressure in chamber. 21, which in turn reduces thepressure diiferential between: tank 25 and chamber 21, thereby reducingthe flow through line 26 to restore the liquid level in the chamber. I

By proper selection of pressure conditions in chamber 21, with respectto other conditions obtaining, including the supplying of heat to theliquid from the atmosphere or otherwise, if required, any desiredproportion of-the materialpassed from storage may be evaporatedand'bledoff from the chamber as vapor through connection 30. The proportion ofvapor phase thus formed and separated may preferably be a minor portion:of' the material leaving storage. but if desired theimajor portion maybe thus :separated aswapor phase material, a minor portion being passed.asliquid through .the liquid meter. With commercial liquid propane, upto approximately 5.0% of the liquid :may be evaporatedibyexpansiondownrto atmospheric pressure without requiring the supply of extraneousheat. Since "with the evaporation ;of :any considerable proportion ofthe liquid, the temperature of the remaining liquid will be reduced wellbelow the ambient temperature, heat for further evaporation may beconveniently supplied from the atmosphere.

=I-n many :cases.zsu.ch as inzthe'use 'of theinvention particularlydescribed, after the separated liquid phase material has beensmeteredthereis no need to inhibit the vaporization thereof. In the. use. ofliquefied normally gaseous .hydrocarbons, such as hydrocarbons of from:3 to 4 carbon atoms per molecule, the manufacture of combustible gasthe liquefied hydrocarbon-material is. to be vaporizedinthe process in:any event.

The invention usefully employs "the'evaporation of a portion oftheliquefied-hydrocarbon material to: permit the, conveying of theremainder in liquid phase to the proximity of the zone of .itsutilization and its accurate metering.

The vapor phase material separated in chamber-.21, may also beaccuratelymetered prior to use. If desired, baffles or other phase contactingmeans, such for example as rfactionating column. packing, may :beemployed if desired-to remove entrained. liquid phase material from theseparated vapor phase prior to the metering of the, latter.

As a. specific example of the-operation of the invention, liquefiedpropane in .-a storage tank under a temperature --of about 30 F. and.nnder a. pressure of about 100 pounds-per square inch absolute pressureand having an enthalpy of about 123 B. t. u. per pound is passed througha line 4 inches in diameter to a phaseseparating chamber with a pressuredrop en route of about 440 pounds per square inch, with anevaporation ofabout of the material and a drop in temperature to about -1- F.

The separated vapor phase material is bled-off to.-.the gas take-on mainserving-six carburetted Water .gas. sets.

The separated liquid-phase material-is pumped by a booster pump under anincrease in pressure of about. 50- pounds .per square inch through alinchline-about 200 it. long and thence through six-2 inch lines about1.00 it. long to six-liquid meters, under ambient temperature conditionsoiabout 120? F., the-metered material-going to thesi-x Bil-rt. diameterwater gas sets during. the back-mun periodof the .cycleoteachset.

Approximately mgallonsof propaneper cycle issupplied to each of theisixsets with about 1-10. cyolesperhour. About65% of the propane suppliedisreformed by passagethrough the :fuel beds iofnthe generators of therespective sets, being supplied thereto during the back-run" with theback-run steam to the super-heater topsot the several sets. Abo ut.35 ofthe propane is .used as *enrichment" not :being-reformed, includingpropane vapor remaining in thegenerator top, carburetter and"superheater at theend of the: back-run as wellas the separated vaporphase material bled :into' the gas take-off main.

finder the increased pressure supplied .by the :pump, :the ambienttemperature .at the liquid: :meter :is well. below the boiling point or8 the liquid :propane :being metered, and no sub stantial volume ofvapor phase material .is :presout to impair the accuracy of-the meteringtaper-- ation.

i In the employmentof the invention-in connection with'the operation ofa considerable number ofcarburetted water gas sets, due to staggering ofthe cycles of the individual gas sets, pump 33 may be continuouslypumping separated liquid phase hydrocarbon material from the separator 2to the liquid header 36, the liquid flowing therefrom continuouslythrough at least one liquid meter. In a case in which the invention isemployedin connection with the operation of only one carburetted watergas set, the ,flow of liquidhydrooarbon material from thephase separator21 through thev liquid meter will normally be discontinuous, the. flowtaking place during only a certain period or periods in the gasmakingcycle. In such case, the refrigeration and the repressuring of theseparated liquid phase material should preferably be such as to maintainthe material in the line from the pump to and through the liquid meterin liquid phase during the period or periods of the cycle in which thereis no flow of material through line 35. In using the inventionin-connection with the operationofonly a few water ,gas sets, the nowofliquid material from pump 33 may likewise :be discontinuous, althoughnot to such arr-extent as in the case of the operation of only one gasset and therefore the same, considerations may apply but to a lesserdegree.

Referring to Figure .2:

This .figure illustrates another form of the invention. ,Pipelflfl leadsfrom a storage tank (not shownl, which may be similar to tank 25inFigure 1 containing. liquid propane, under the pressure resulting fromstorage under atmospheric temperature conditions.

The liquid propane passes through pipe Hill to the heat exchanger [01 inresponse to pressure differential therebetween.

The heat exchanger is "illustrated as provided with upper and lower tubesheets I02 and I03 respectively and with the tubes I04 extendingtherebetween.

The liquidpropane containing some vapor, produced due to; pressuredropin pipe I00, enters the heat exchanger by way of the space above theupper tube. sheet and flows downwardly through thetubes and thence by'wayof the space below-the lower tube sheet, the connection H15, liquid-meter H116, and connection 101, to a car-' buretted water gas set (notshown). For example, the utilization of the liquid propane in the gasmanufacturing apparatus may 'be asshown anddescribed'in connection withFigure 1,

The flow-of the liquid propane from storage to valve .0, the resultingchilled vapor, passing into the-lower portion of the space between thetube sheets of heat exchanger HH, and back and forth between bafilessuchas Hlla, cools the mixture-of :liquid propane and propane vapor Ipassedintozthe heat exchanger above the upper tube sheet.

This results in .the condensation- IIII is provided with means foradjusting its opening, and in operation suflicient liquid propane isexpanded therethrough, to reduce the temperature of the liquid propaneissuing from the base of the heat exchanger, sufficiently low as toensure the absence of any substantial.

volume of vapor phase therein during metering;-

The propane vapor bled off through expansion valve I I0, passes out ofthe heat exchanger by way of connection III, and is passed through thevapor meter II2, from whence it passes, by way of connection H3, to thegas take-off main II I, which may be connected to one or more gas sets(not shown) in similar manner to take-off main 23 in Figure 1.

Expansion valve IIEI is illustrated as operated by hydraulic cylinderH5, which may be actuated by the automatic control machine (not shown)of the carburetted water gas set, so as to be moved toward the wide-openposition simultaneously with the opening of valve H13, in line II".

If desired, the operation of valve III} may be arranged so that it doesnot entirely close, thereby bleeding oii through the valve a smallproportion of propane, to provide refrigeration in the heat exchangerduring periods of the water gas cycle when valve I08 is closed. Toreduce loss of refrigeration the heat exchanger is illustrated as laggedwith the heat insulating material H6.

In the form of the invention illustrated in.

Figure 2, the vaporization of an additional proportion of the liquidpropane permits the omission of the step of repressuring the liquidpropane prior to passage through the liquid meter. If the additionalvapor cannot be conveniently utilized, as for cold enrichment asdescribed, any desired proportion oi the vapor leaving the heatexchanger may be compressed, after cooled and returned to storage asliquid. The same procedure may be followed, if desired, in the case ofany proportion of the separated vapor phase material from the phaseseparator of Figure 1.

Referring to Figure 3:

Figure 3 shows the upper portion of the apparatus of Figure 2, modifiedsomewhat to provide for the periodic removal of uncondensed gas from theupper portion of the heat exchanger should such gas tend to accumulate.

As in Figure 2, I indicates the pipe leading from the liquid propanestorage. IIJI is the heat exchanger generally. IE2 is the upper tubesheet, I04 the tubes, IIOa a baille, and He the insulating lagging ofthe heat exchanger. III is the vapor line leading through vapor meter H2and connection I I3 to utilization of the vapor, such as by admission tothe gas take-01f main (not shown).

In the modified apparatus of Figure 3, a bleeder connection I isprovided leading from the upper portion of the space above the uppertube sheet to connection III. The bleeder connection is illustrated asprovided with two valves I2I and I22 arranged in series.

Pressure actuated valve I2I is operatively connected by way of pipes I26and I23 with the space above the upper tube sheet and is arranged toremain closed when the pressure in said space is below a predeterminedvalue, and to open when said pressure is above said predetermined value.Valve I22 is operatively con- .10 I nected with float I24, in suchmanner that whe the float is maintained in its uppermost position by theliquid in the space above the tube sheet, the valve I22 is in the'closedposition, but when a lower level of liquid causes a falling of thefloat, valve I22 is moved toward the open position. v Y

As a resultof these provisions, if a sufficient body of uncondensed gasaccumulates in the top of the'heat exchanger, under the'storagepressureless the line drop, both valves will be opened and the gas automaticallybled oif. Thev refilling of the space above the upper tube sheet withliquid raises the float and closes valve I22. Due to provision of valveI2I pressure inthe topof the heat exchanger will not be unduly reducedwith the consequent flashing-off .of unnecessary proportions of theliquid. j f

As previously stated, the invention is capable of many otherapplications than the specific application particularly described above.It may readily find use in the handling andiutilization of othernormally gaseous hydrocarbons .than propane and butane, such for exampleas ethane, ethylene, propylene, butylenes and others. Moreover, it maybe applied to the handling of volatile liquids, other than hydrocarbons,such for example as methyl chloride, boiling point 24 0., methyl amine,boiling point '6.7"C., vinyl chloride, boiling point -12 C. and others.

I The invention is not limited to use with organic liquids as it may bereadilyapplied to the'handling of such materials as liquid anhydrousammonia, boiling point -33? C. and to superheated water. g

The invention is applicable to the piping and metering of liquid phasematerial containing two or more constituents, one or more of which maytend to separate as vapor phase from the remainin liquid material upondrop in pressure under the ambient temperature conditions. Included-isliquid phase material relatively non-volatile .at atmospheric pressureunder the temperature conitions obtaining and containing dissolvedmaterial which is gaseous at atmospheric pressure under the temperatureconditions obtaining and maintained in liquid phase by elevatedpressure. Such liquid phase materials include, forexample, aqueousammonia and carbonated liquids.

The invention has particular advantages in its the utilization ofliquefied normally gaseous hydrocarbon material in the manufacture ofcombustible gas, for example, in a carburetted water gas set, aspreviously described and otherwise. In such use, separated vapor phasematerial bled off from the phase separating chamber may be veryconveniently employed in the gas-making operation, as Well as theseparated liquid material. This vapor phase material may be bled intothe gas take-off main, as previously described, at any period in thecyclic operation of any gas set connected therewith, or maybe passed.into any set during any desired gas-making period, for purposes ofenrichment with little or no cracking or to be reformed bypassagethrough the fuel bed, Withcracking therein to lighter hydrocarbonmaterial, hydrogen, and carbon.

In the claims the expressions substantial volume of vapor phasematerial, substantial volume of vapor phase hydrocarbon material andsimilar expressions are intended t mean volumes of vapor such as 'toafiect the accuracy of metering of the liquid phase material'beyond thelimits of reasonable tolerance. It is obvious that from this standpointthe lower the proportion 11 201 vapor phase fin fizhe material passingthrough lcheiliquid :meter the :better. :Itiis likewise obvious '#thatone itolerances as ;to meter :accuracy Jmay widely .as :betweendifferent uses of the :in-

wention. Preferably the proportion of yapor iphase accompanying theliquid phase material when metered should be less than "thereofzbyouolume, more preferably :should .bBIleSS than 53% fthereof, :and.still more preferably less than 1 or even 11% ithereoi. :In :the .case:of normally gaseous hydrocarbons these :proportions :repre- 35-56111the evaporation of extremely .small proporitions by weight. The:invention, however, is :not necessarily :Iimited to the presence of any-:pa.rtlcular proportion f vapor :phase .material with rthe liquid phaseundergoing metering.

. fflther 'Jnodifications may readily :occur 1110 those skilled in theart without departing from the spirit :0! :the :present invention, whichis intended befiimited only as required by :the appended .-:elalmsandzthe priorzart.

swesclaimz' ll. illheimethod 10f distributing normally :gasenushydrocarbon-material employed in-the manuitac'turerof combustible:gasiby a ,process involvring alternate iheatingiof contact material in.a

sizes-generating .set and passing hydrocarbon and =ssteam ftherethrouglhin a :cyclic operation, comprising flowing said liquefied normallygaseous hydrocarbon material from iaicontainer in which :mressureconditions are :such as to maintain said momnazlly gaseous material-substantially in the illiquid :p'hase "thereinunder the temperatureconiiitions obtaining, I along a confined path in which pressureconditions are reduced with respect 'to xsaildcontainer to cause flowfrom said container and to cause partial conversion of said liquefied:mormally gaseous hydrocarbon material to "the wapor phase \wi'th thechilling of the "remaining iliquid phase material, to a confined-phasesepasrating :zone; withdrawing vapor phase material;

flowing said chilled liquefied normally gaseous hydrocarbon materialfrom said phase separating-zone along :a second confined path to anda'liquid meter at an increased pressure with respect to said phaseseparating zone such fihat the temperature of said chilled liquefiednormally gaseous hydrocarbon material in said second confined path isbelow its boiling point thereim tl-1ereaiter passing said meteredhydrocarbon material with steam through 'said -hot montact material ofsaid gas-generating set to produce combustible gas.

2. The method of utilizing normally gaseous mydrocarbon mater-ialemployed the manufac- '?bon substantially in :the liquid state therein:un-

der the -.temperature conditions obtaining, which =-comprises conductingsaid liquefied normally gaseous hydrocarbon along .a confined path inwhich mhe pressure :conditions are reduced :with reenest rte saidcontainer to cause flow from said pontainer and to cause partialconversion of said :liquefied normally gaseous hydrocarbon material atethe :vapor phase with the chilling of the remaining liquefied normallygaseous hydrocarbon 12 *materiaht .a :confined phase separating :zone;withdrawing zan'd :metering the mesultingseparated vapor iphasehydrocarhonzmaterialzso{asfto maintain approximately constant liquidzlevel in said phase separating :zone; iflowing said achilled liquefied:normally gaseous hydrocarbon :material from said :phase :separatingzone along a second confined :path to :and through a .liquidmeterat anincreased pressure with respect :to :said phase separating zone such:that ithe temperature of said chilledji-quefiod normally gaseous.imaterial in ZBEj-dISECOIld .confmed :path is below its boiling pointtherein; thereafter passing said lhydrocarbon material which was meteredrindiquid phase through said heated contact material 'in the :presence"of steam during ;a gas-making period of said cycle, and mixing lWith:combustible gas thereby produced said vaporiphase'lhydroear- :bonmaterial which was separately metered in wapor phase.

3. apparatus for distributing i'liquified normally gaseous hydrocarbonmaterialz in 'the manufacture-of combustible gas ina gas-making set,including asg'as-making generator adapted to contain hot contactmaterial, said liq'uified normally gaseous :materia'l subjected, wduring:dis- :tribution, :to pressure :and temperature conditions whichcausepartial :gasizfication thereof, [comprisingxa apressure storage tank, :aconduit Heading *iromcsaid rta'nk :to a confined phase separatingchamber, a pressure reducing valve insa'id con- ;duit responsive to:pressurefiin said xphase separating chamber and adapted to closesaidconduit when the pressure in said phase separatingc'ham- 'ber exceeds apredetermined pressure, a second conduit-connected to the upperpartofsaid chamber for leading vapor "phase material therefrom, a :floatadapted :to rise and fall with the devel .of the liquid in :said phaseseparating chamber and :operatively@connectedwith the valve-in saidsecond conduit wlriereby said valve is moved to- -ward the closedposition upon the rise *of .said liquid level :and toward the open:position upon :the fall of said liquid ileveL a third conduitcon-'nected to the lower part of said phase-separating chamber and in fluidflow communication with said .igas-making generator, said :third conduithaving a pump and a liquid meter therein, said pump being locatedbetween said phase separating chamber and saidtmeter.

1. .An apparatus "for distributing liquifiednormallygaseous hydrocarbonmaterial in the manufacture of combustible gas in a :gas making set,includinga gas-makinggeneratoradapted to-con- 'tain hotcontact material,and gas take-off means leading to .a-qgaszstorage vessel, said iiquified'normally gaseous material subjected, during distribution, .to pressureand temperature-condi- 'it'iODS which cause partial :gasification:thereof, comprising a pressure storage tank, -a conduit leading fromsaid :tank to :a oonfined phase separating chamber, a pressure reducingya lve in said conduit :responsive to pressure in -se 'id phaseseparating chamber and adapted to :close said conunit when the pressuresaid phase separating chamber exceeds a predetermined pressure, a secondconduit connected 'to the upper part of said chamber for leading vaporphase material therefrom and in fluid flow communication with said gastake-off means, a vapor meter located in said second conduit, a floatadapted to rise and fal-l'with the level ofthe liquid in said phaseseparating chamber and operatively connected with the valve in saidsecond conduit whereby said valve is moved toward the closed positionupon the rise of said liquid level and toward the open position upon thefall of said liquid level, a third conduit connected to the lower partof said phase separating chamber and in fluid flow communication withsaid gas-making generator, said third conduit having a pump and a liquidmeter therein said pump being located between said phase separatingchamber and said meter.

JOHN S. HAUG.

PRICE W. JANEWAY, JR.

REFERENCES CITED The following references are of record in the file ofthis patent:

Number 14 UNITED STATES PATENTS Name Date Rose Feb. 16, 1926 Huif Dec.13, 1927 Rosenthal Apr. 12, 1932 Faber July 18, 1933 Young Sept. 25,1934 Marden Sept. 3, 1935 De Motte Mar. 3, 1936 Young Sept. 22', 1936Werts May 6, 1941 Benz et a1 Aug. 4, 1942 Hirsch Dec, 29, 1942

1. THE METHOD OF DISTRIBUTING NORMALLY GASEOUS HYDROCARBON MATERIALEMPLOYED IN THE MANUFACTURE OF COMBUSTIBLE GAS BY A PPROCESS INVOLVINGALTERNATE HEATING OF CONTACT MATERIAL IN A GAS-GENERATING SET ANDPASSINNG HYDROCARBON AND STEAM THERETHROUGH IN A CYCLIC OPERATION,COMPRISING FLOWING SAID LIQUEFIED NORMALLY GASEOUS HYDROCARBON MATERIALFROM A CONTAINER IN WHICH PRESSURE CONDITIONS ARE SURE AS TO MAINTAINSAID NORMALLY GASEOUS MATERIAL SUBSTANTIALLY IN THE LIQUID PHASE THEREINUNDER THE TEMPERATURE CONDITIONS OBTAINING, ALONG A CONFINED PATH INWHICH PRESSURE CONDITIONS ARE REDUCED WITH RESPECT TO SAID CONTAINER TOCAUSE FLOW FROM SAID CONTAINER AND TO CAUSE PARTIAL CONVERSION OF SAIDLIQUEFIED NORMALLY GASEOUS HYDROCARBON MATERIAL TO THE VAPOR PHASE WITHTHE CHILLING OF THE REMAINING LIQUID PHASE MATERAL, TO A CONFINED PHASESEPARATING ZONE; WITHDRAWING VAPOR PHASE MATERIAL FLOWING SAID CHILLEDLIQUEFIED NORMALLY GASEOUS HYDROCARBON MATERIAL FRON SAID PHASESEPARATING ZONE ALONG A SECOND CONFINED PATH TO AND THROUGH A LIQUIDMETER AT AN INCREASED PRESSURE WITH RESPECT TO SAID PHASE SEPARATINGZONE SUCH THAT THE TEMPERATURE OF SAID CHILLED LIQUEFIED NORMALLYGASEOUS HYDROCARBON MATERIAL IN SAID SECOND CONFINED PATH IS BELOW ITSBOILNG POINT THEREIN; THEREAFTER PASSING SAID METERED HYDROCARBONMATERIAL WITH STEAM THROUGH SAID HOT CONTACT MATERIAL OF SAIDGAS-GENERATING SET TO PRODUCE COMBUSTIBLE GAS.